CN221513549U - Methanol rectifying system - Google Patents
Methanol rectifying system Download PDFInfo
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- CN221513549U CN221513549U CN202420021295.XU CN202420021295U CN221513549U CN 221513549 U CN221513549 U CN 221513549U CN 202420021295 U CN202420021295 U CN 202420021295U CN 221513549 U CN221513549 U CN 221513549U
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- tower
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- side extraction
- column
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- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 318
- 238000000605 extraction Methods 0.000 claims abstract description 35
- 238000009835 boiling Methods 0.000 claims description 22
- 238000005086 pumping Methods 0.000 claims description 19
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 239000000446 fuel Substances 0.000 claims description 7
- 239000000126 substance Substances 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 2
- 239000000498 cooling water Substances 0.000 claims 1
- 238000010992 reflux Methods 0.000 description 26
- 239000007789 gas Substances 0.000 description 19
- 239000007788 liquid Substances 0.000 description 11
- 239000000047 product Substances 0.000 description 11
- 238000011084 recovery Methods 0.000 description 9
- 238000000034 method Methods 0.000 description 8
- 239000012071 phase Substances 0.000 description 8
- 239000006227 byproduct Substances 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 239000007791 liquid phase Substances 0.000 description 4
- 238000000926 separation method Methods 0.000 description 4
- 239000012530 fluid Substances 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 238000001816 cooling Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 150000002170 ethers Chemical class 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 150000004702 methyl esters Chemical class 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 238000003786 synthesis reaction Methods 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 239000013064 chemical raw material Substances 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000003068 static effect Effects 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a methanol rectifying system which comprises a light component removing tower, a pressurizing tower, an atmospheric tower and a side extraction tower, wherein the operating pressure of the atmospheric tower is approximately equal to that of the side extraction tower, the atmospheric tower is connected with a feed inlet of the side extraction tower through a side extraction pipeline of the atmospheric tower, the side extraction pump is arranged on the side extraction pipeline of the atmospheric tower, and a methanol-rich product extracted from the top of the side extraction tower is recycled to the feed inlet of the atmospheric tower for continuous rectification.
Description
Technical Field
The utility model relates to the technical field of rectification, in particular to a methanol rectification system.
Background
Methanol is not only an important basic chemical raw material, but also clean energy and power fuel with excellent performance, and has important effects in increasingly emphasizing environmental protection, energy conservation and emission reduction. The method for synthesizing the methanol generally used at present takes coal as a source, and finally obtains a methanol product through gasification, low-temperature methanol washing, gas separation and methanol refining units. The methanol rectifying unit is used as a core unit for refining methanol, so that the reduction of equipment cost and process energy consumption is of great significance to optimizing the whole methanol manufacturing process.
CN1328232C discloses a double-effect rectification energy-saving water-saving system and process for methanol. The system comprises a pre-rectifying tower, a pressurizing tower, an atmospheric tower and a methanol recovery tower. The side offtake pipe of the atmospheric tower is connected with the feed inlet of the recovery tower, and the side offtake pipe of the atmospheric tower is used for offtaking medium-concentration steam materials and enters the recovery tower by static pressure difference. Refined methanol products are extracted from the top of the recovery tower, and waste liquid discharged from the bottom of the recovery tower can be used as extraction water of the pre-rectifying tower. In order to directly extract refined methanol product from the top of the tower, the methanol recovery tower has a large volume and enough tower plates to meet the rectification requirement.
In view of this, how to design a new methanol rectification system, which can recover methanol and reduce the investment cost of the recovery tower at the same time, is a problem to be solved by related technicians in the industry.
Disclosure of utility model
In order to realize recovery of methanol in a mixed stream extracted from an atmospheric tower by a fourth tower with small volume and few tower plates, the utility model discloses a methanol rectifying system, which comprises a light component removing tower, a pressurizing tower, an atmospheric tower and a side extraction tower, wherein the operating pressures of the atmospheric tower and the side extraction tower are approximately equal, the atmospheric tower is connected with a feed inlet of the side extraction tower through a side extraction pipeline of the atmospheric tower, and a side extraction pump is arranged on the side extraction pipeline of the atmospheric tower.
Optionally, a pressure reducing valve is arranged at one end of the side extraction pipeline of the atmospheric tower close to the side extraction tower, and the side extraction tower is a fourth tower for realizing the methanol recovery function.
In one aspect, the system further comprises a conduit for condensing and pressurizing the methanol-rich product withdrawn from the side draw column and returning it to the atmospheric column.
In yet another aspect, the system further comprises a conduit for cooling the water and high boilers at the bottom of the side draw to the boundary region for fueling. Or the system can be arranged to comprise a side draw line connected to the lower portion of the side draw for delivering the drawn fusel to the boundary region for fueling; and a pipe for discharging water at the bottom of the side draw tower.
Compared with the prior art, the technical scheme provided by the utility model has the following advantages:
1. The system increases methanol production by about 0.11% compared to the absence of the side draw column.
2. The mixed stream from the atmospheric tower entering the side draw tower is pressurized and then expanded to produce a flash-like effect to promote the separation of methanol and water from the fusel in the side draw tower.
3. And the methanol-rich product extracted from the top of the tower is refluxed to the normal pressure tower for rectification again, so that the requirements on the rectification efficiency of the side extraction tower are reduced. And the method is combined with the advantage 2, so that the recycling of the methanol can be realized by using the side-pumping tower with smaller volume.
Drawings
The advantages and spirit of the present utility model will be further understood from the following detailed description and drawings, and those skilled in the art will recognize that the drawings and examples do not limit the present utility model in any way.
FIG. 1 is a schematic diagram of the methanol rectification system in example 1.
FIG. 2 is a schematic diagram of the methanol rectification system of example 2.
In the figure: 1. crude methanol; 2. an expansion tank; 3. a light ends column reboiler; 4. a light component removing tower; 5. a pressurized column reboiler; 6. a pressurizing tower; 7. a condensing evaporator; 8. a pressurized tower reflux drum; 9. a pressurized tower reflux pump; 10. a light component removal tower condenser; 11. a light component removal tower reflux drum; 12. a reflux pump of the light component removing tower; 13. an exhaust gas cooler; 14. an atmospheric tower; 15. a condenser of the atmospheric tower; 16. a reflux drum of the atmospheric tower; 17. a reflux pump of the atmospheric tower; 18. a side pump; 19. a subcooler; 20. a side extraction tower; 21. a side draw reboiler; 22. a side draw condenser; 23. a side extraction tower reflux drum; 24. a side-pumping tower reflux pump; 25. a side offtake pipeline of the atmospheric tower; 26. side extraction pipeline of side extraction tower
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the present application more apparent, the technical solutions of the present application will be clearly and completely described below with reference to the accompanying drawings, and it is apparent that the described embodiments are some embodiments of the present application, but not all embodiments. All other embodiments, based on the examples of the application, which a person of ordinary skill in the art would achieve without inventive faculty, are within the scope of the application.
In the description of the present application, it should be noted that the terms "mounted," "connected," and "connected" are to be construed broadly, unless otherwise specifically defined and limited. "fixedly connected" or "secured to" or "non-movably connected" means that the connection between two or more structural members is not configured to provide relative movement. Examples of fixed connections include welded connections, flanged connections, or bolted connections.
Furthermore, the appearances of the phrase "a" or "an" in this document are not meant to be limiting, but rather, describe features that have not been apparent from the foregoing description. Likewise, unless a particular quantity of a noun is to be construed as encompassing both the singular and the plural, both the singular and the plural may be included in this disclosure.
It should be understood that in the present application, "at least one (item)" means one or more, and "a plurality" means two or more. "and/or" is used to describe association relationships of associated objects, meaning that there may be three relationships, e.g., "a and/or B" may mean: only a, only B and both a and B are present, wherein a, B may be singular or plural. The character "/" generally indicates that the context-dependent object is an "or" relationship. "at least one of" or the like means any combination of these items, including any combination of single item(s) or plural items(s). For example, at least one (one) of a, b or c may represent: a, b, c, "a and b", "a and c", "b and c", or "a and b and c", wherein a, b, c may be single or plural.
The terms "upper", "lower", "upper" and "lower" are made with respect to the relative orientation of the device in the operating state.
The crude methanol refers to methanol, water, dissolved gas and other trace by-product impurities, wherein one part of the crude methanol has a boiling point lower than that of the methanol, and the other part of the crude methanol has a boiling point higher than that of the methanol, and the purpose of rectification is to remove the trace impurities to meet the purity requirement of refined methanol. Taking the methanol standard (GB 338-2011) for the Chinese industry as an example, the mass fraction of water in refined methanol is less than or equal to 0.10 percent, and the mass fraction of acid is less than or equal to 0.0015 percent.
By "column" is meant herein a hollow structure capable of sufficient contact and mass transfer of gas and liquid, and if desired, may be fitted with packing to promote contact of the gas with the liquid. The towers are in fluid connection through pipelines.
The pressures herein are absolute pressures.
Example 1
The methanol rectifying system shown in fig. 1 includes 4 columns, namely, a light component removing column 4 for removing low-boiling components, a pressurizing column 6 for removing high-boiling components, an atmospheric column 14 and a side-draw column 20 for recovering methanol. The crude methanol 1 from the synthesis section is first flashed in expansion tank 2 to about 5barg and the flash stream is sent out of the boundary zone via a pressure control valve for fuel, and the flashed methanol is flow controlled to the rectification section.
In the rectification section, the flashed crude methanol first enters a light ends column 4, the heat duty of which is provided by a light ends column reboiler 3. The crude methanol still contains partially dissolved gases such as CO 2 and CH 4, etc., which are mixed with low boiling substances (ethers and methyl esters) in a large amount of methanol vapor and removed overhead. The gas phase at the top of the tower flows back through a light component removal tower condenser 10, most of methanol is condensed and recycled to a light component removal tower reflux tank 11, and then is sent to the top of the tower through a light component removal tower reflux pump 12. The noncondensable gas is recycled to the reflux tank 11 of the light component removal tower through the exhaust gas cooler 13, and the residual gas phase is sent out of the boundary region and can be used as fuel gas.
The temperature of the crude methanol entering the light ends column 4 is about 40 ℃, the pressure is about 5.6barg, and after the removal of low boilers, the temperature of the stabilized methanol leaving the bottom of the light ends column is about 90 ℃ and the pressure is about 2.4barg. The pressure of this methanol stream was raised to about 9.8barg and fed to the pressure column 6. The high boiling by-products (mainly high boiling ethanol and water) are separated from the methanol in the pressurization column 6 and the atmospheric column 14. Wherein about 50% of the pure methanol comes from the rectification of the pressure column 6. The vapor (mainly methanol) at the top of the pressurizing tower is condensed by a condensing evaporator 7, the heat provided by the condensation is used for reboiling the liquid in an atmospheric tower 14, and the methanol condensate is collected in a pressurizing tower reflux drum 8. Part of the methanol condensate is returned to the top of the pressure tower by the pressure tower reflux pump 9, and the rest of the methanol is further cooled in the subcooler 19 and sent out as a product to the boundary zone. The heat duty of the pressure column 6 is provided by the pressure column reboiler 5.
The methanol containing high-boiling byproducts left at the bottom of the pressurizing tower flows into the atmospheric tower 14 under the control of the liquid level to continue rectification. The methanol stream is fed to the atmospheric tower 14 at a temperature of about 134 c and a pressure of about 8.6barg, after depressurization. The atmospheric tower 14 operates under atmospheric conditions and functions similarly to the pressurized tower 6. The methanol vapor at the top of the atmospheric tower is condensed by an atmospheric tower condenser 15 and then is collected in an atmospheric tower reflux tank 16. A part of the methanol is returned to the top of the atmospheric tower by an atmospheric tower reflux pump 17, and the other part is sent out of the boundary zone as a product. The bottom of the atmospheric tower is mainly water which is cooled by a process water pump through liquid level control and then sent to a boundary region.
In order to reduce the concentration of high boiling impurities at the bottom of the atmospheric tower and meet the discharge requirement of process wastewater, a certain amount of fusel is extracted from the lower part of the atmospheric tower 14 along an atmospheric tower side extraction pipeline 25. The temperature of the side-draw fusel is about 92℃and the pressure is about 1.78bara, and after the pressure has been raised to about 5.9bara by side-draw pump 18, it is fed to side-draw column 20. Since the side draw column 20 operates at a pressure similar to that of the atmospheric column 14, the pressure of the mixed fluid in line 25 is substantially higher than that of the side draw column 20, and when it enters the side draw column 20, flash-like phenomena occur due to sudden depressurization and expansion, and the lower boiling component, i.e., methanol, is enriched in the gaseous state. Or on the pipeline 25, after the side pumping pump 18 and before the feed inlet of the side pumping tower 20, a pressure reducing valve is arranged, the mixed liquid is flashed when flowing through the pressure reducing valve, so as to obtain a gas phase rich in methanol and a liquid phase with lower methanol content, and the gas phase and the liquid phase are separated after entering the side pumping tower 20. Either way, the fusel from the atmospheric tower 14 is initially separated when entering the side draw tower 20.
In the side draw column 20, 60% of the methanol was recovered. The methanol-rich product at the top of the side-pumping tower is condensed by a side-pumping tower condenser 22 and is collected in a side-pumping tower reflux tank 23. A portion is returned to the side draw column 20 via a side draw reflux pump 24 and the remainder is recycled to the atmospheric column 14. The bottom of the side pumping tower is mainly water and high-boiling substances, and the water and the high-boiling substances are cooled and sent to a boundary region to be used as fuel. The heat duty of the column is provided by a side draw reboiler 21. Since the side draw column 20 does not directly produce refined methanol, its separation efficiency only needs to be achieved to recover most of the methanol. For a system capable of handling 3000 tons/day of crude methanol, the side draw column 20 may be a 1m diameter column with a 9m height, saving capital investment in equipment.
Example 2
The methanol rectifying system shown in fig. 2 includes 4 columns, namely, a light component removing column 4 for removing low boiling components, a pressurizing column 6 for removing high boiling components, an atmospheric column 14 and a side draw column 20 for recovering methanol. The crude methanol 1 from the synthesis section is first flashed in expansion tank 2 to about 5barg and the flash stream is sent out of the boundary zone via a pressure control valve for fuel, and the flashed methanol is flow controlled to the rectification section.
In the rectification section, the flashed crude methanol first enters a light ends column 4, the heat duty of which is provided by a light ends column reboiler 3. The crude methanol still contains partially dissolved gases such as CO 2 and CH 4, etc., which are mixed with low boiling substances (ethers and methyl esters) in a large amount of methanol vapor and removed overhead. The gas phase at the top of the tower flows back through a light component removal tower condenser 10, most of methanol is condensed and recycled to a light component removal tower reflux tank 11, and then is sent to the top of the tower through a light component removal tower reflux pump 12. The noncondensable gas is recycled to the reflux tank 11 of the light component removal tower through the exhaust gas cooler 13, and the residual gas phase is sent out of the boundary region and can be used as fuel gas.
The temperature of the crude methanol entering the light ends column 4 is about 40 ℃, the pressure is about 5.6barg, and after the removal of low boilers, the temperature of the stabilized methanol leaving the bottom of the light ends column is about 90 ℃ and the pressure is about 2.4barg. The pressure of this methanol stream was raised to about 9.8barg and fed to the pressure column 6. The high boiling by-products (mainly high boiling ethanol and water) are separated from the methanol in the pressurization column 6 and the atmospheric column 14. Wherein about 50% of the pure methanol comes from the rectification of the pressure column 6. The vapor (mainly methanol) at the top of the pressurizing tower is condensed by a condensing evaporator 7, the heat provided by the condensation is used for reboiling the liquid in an atmospheric tower 14, and the methanol condensate is collected in a pressurizing tower reflux drum 8. Part of the methanol condensate is returned to the top of the pressure tower by the pressure tower reflux pump 9, and the rest of the methanol is further cooled in the subcooler 19 and sent out as a product to the boundary zone. The heat duty of the pressure column 6 is provided by the pressure column reboiler 5.
The methanol containing high-boiling byproducts left at the bottom of the pressurizing tower flows into the atmospheric tower 14 under the control of the liquid level to continue rectification. The methanol stream is fed to the atmospheric tower 14 at a temperature of about 134 c and a pressure of about 8.6barg, after depressurization. The atmospheric tower 14 operates at atmospheric conditions and functions similarly to a pressurized tower. The methanol vapor at the top of the atmospheric tower is condensed by an atmospheric tower condenser 15 and then is collected in an atmospheric tower reflux tank 16. A part of the methanol is returned to the top of the atmospheric tower by an atmospheric tower reflux pump 17, and the other part is sent out of the boundary zone as a product. The bottom of the atmospheric tower is mainly water, and is fed into the middle lower part of the side-pumping tower 20 through liquid level control.
To reduce the concentration of high boiling impurities at the bottom of the atmospheric tower and meet the discharge requirement of process wastewater, a certain amount of fusel is extracted from the lower side line of the atmospheric tower 14. The temperature of the side-draw fusel is about 92℃and the pressure is about 1.78bara, and after the pressure has been raised to about 5.9bara by side-draw pump 18, it is fed to side-draw column 20. Since the side draw column 20 operates at a pressure similar to that of the atmospheric column 14, the pressure of the mixed fluid in line 25 is substantially higher than that of the side draw column 20, and when it enters the side draw column 20, flash-like phenomena occur due to sudden depressurization and expansion, and the lower boiling component, i.e., methanol, is enriched in the gaseous state. Or on the pipeline 25, after the side pumping pump 18 and before the feed inlet of the side pumping tower 20, a pressure reducing valve is arranged, the mixed liquid is flashed when flowing through the pressure reducing valve, so as to obtain a gas phase rich in methanol and a liquid phase with lower methanol content, and the gas phase and the liquid phase are separated after entering the side pumping tower 20. Either way, the fusel from the atmospheric tower 14 is initially separated when entering the side draw tower 20.
In the side draw column 20, 60% of the methanol was recovered. The methanol-rich product at the top of the side-pumping tower is condensed by a side-pumping tower condenser 22 and is collected in a side-pumping tower reflux tank 23. A portion is returned to the side draw column 20 via a side draw reflux pump 24 and the remainder is recycled to the atmospheric column 14. The lower portion of side draw 20 draws a stream of fusel along side draw sidedraw draw line 26 and out of the boundary as fuel, the bottom being primarily water, and after cooling, as process effluent exiting the boundary. The heat duty of the column is provided by a side draw reboiler 21. Since the side draw column 20 does not directly produce refined methanol, its separation efficiency only needs to be achieved to recover most of the methanol. For a system capable of handling 3000 tons/day of crude methanol, the side draw column 20 may be a 1m diameter column with a 9m height, saving capital investment in equipment.
The preferred embodiments of the present utility model have been described in the specification, and the above embodiments are merely illustrative of the technical solution of the present utility model and not limiting thereof. Each aspect or embodiment defined herein may be combined with any other aspect or embodiment unless clearly indicated to the contrary. In particular, any feature indicated as being preferred or advantageous may be combined with any other feature or features indicated as being preferred or advantageous. All technical solutions that can be obtained by logic analysis, reasoning or limited experiments according to the inventive concept by those skilled in the art shall be within the scope of the present utility model.
Claims (6)
1. A methanol rectification system, characterized in that: the device comprises a light component removing tower, a pressurizing tower, an atmospheric tower and a side extraction tower, wherein the operating pressure of the atmospheric tower is equivalent to that of the side extraction tower, the atmospheric tower is connected with a feed inlet of the side extraction tower through a side extraction pipeline of the atmospheric tower, and a side extraction pump is arranged on the side extraction pipeline of the atmospheric tower.
2. The methanol rectification system of claim 1, wherein: a pressure reducing valve is arranged at one end of the side extraction pipeline of the atmospheric tower close to the side extraction tower.
3. The methanol rectification system of claim 1, wherein: and a pipeline for condensing and pressurizing the methanol-rich product extracted from the top of the side extraction tower and then returning the condensed and pressurized methanol-rich product to the normal pressure tower.
4. A methanol rectification system as claimed in claim 3, wherein: the side-pumping tower also comprises a pipeline for cooling water and high-boiling substances at the bottom of the side-pumping tower and sending the cooled water and the high-boiling substances to the boundary region for fuel.
5. A methanol rectification system as claimed in claim 3, wherein: the side extraction tower side line extraction pipeline is connected with the lower part of the side extraction tower and is used for sending the extracted fusel to a boundary region to be used as fuel.
6. The methanol rectification system of claim 5, wherein: and a pipeline for discharging water at the bottom of the side pumping tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202420021295.XU CN221513549U (en) | 2024-01-04 | 2024-01-04 | Methanol rectifying system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202420021295.XU CN221513549U (en) | 2024-01-04 | 2024-01-04 | Methanol rectifying system |
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| Publication Number | Publication Date |
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| CN221513549U true CN221513549U (en) | 2024-08-13 |
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| CN202420021295.XU Active CN221513549U (en) | 2024-01-04 | 2024-01-04 | Methanol rectifying system |
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